Method for producing detergent-grade alkylate



r Feb. 4, 1969 I D. B. CARSON ETAL METHOD FOR PRODUCING DETERGENT-GRADE ALKYLATE 4 Filed Nov. 20, 1967 A TTUR/VEYS' United States Patent O 4 Claims ABSTRACT OF THE DISCLOSURE Method for producing detergent-grade alkylate via ni paran separation, n-parafn dehydrogenation to the corresponding mono-olefin, catalytic alkylation of the olefin with benzene, and separation of the desired alkylate product. The lmethod is applicable particularly to the production of alkylbenzenes having a 5-carbon homolog spread, such as C to C14, in the alkyl side-chain.

Background of the invention This invention relates to a combination process for the production of detergent-grade alkylate. It specifically relates to a method for selective separation of suitable nparain feedstocks for charge to a dehydrogenation reaction operating in conjunction with a benzene alkylation unit.

It has long been known that the satisfactory disposal of sewage and the inactivation of detergents dissolved in the sewage is a difiicult but extremely necessary processing problem. Many of the detergents, for example, those having an alkylaryl structure as the organic portion tends-4 to produce stable foams in hard or soft waters in such large quantities that .the foam clogs sewage treatment facilities and often appears in suicient concentration in the s elwage treatment facilities to destroy the bacteria necessary for sucient biological action on the sewage. The prior art has also 4known that the alkylbenzene sulfonates (ABS) detergents which are based on using propylene-tetramer as the alkylating agent for benzenes is relatively non-biode- -gradable and, therefore, usually undesirable in current sewage treatment plants. On the other hand, the prior art has also known that biodegradable linear al-kylbenzene sulfonates (LAB) are extremely satisfactory and most desirable in the commercial market today. Present methods for producing the biodegradable detergents utilize normal paraffin hydrocarbons as a source of the straight-chain alkyl substituents. `One prior art processing scheme for producing LA-B has included: chlorination followed by direct alkylation of benzenes with yalkyl chlorides using aluminum chloride as the catalyst; or chlorination followed by dehydroc-hlorination and alkylation of benzenes with the resultant olens using an acid catalyst; and/ or the cracking of higher molecular weight parainic hydrocarbons, such as waxes, to form suitable olens which are then used to alkylate benzenes with an acid catalyst.

More recently, however, there has been a process accounted in which the normal parans are made in sufcient purity for direct catalytic dehydrogenation of the n-paraflins. to the corresponding n-mono-olens of the same carbon number. Basically, this most recent prior art process involves the extraction of, for example, kerosene to produce n-paratns of extremely high purity. These high purity n-parati'ms are catalytically dehydrogenated to n- 3,426,092 Patented Feb. 4, 1969 mono-olefins. The dehydrogenation eluent is admixed with benzenes and converted to alkylbenzenes in the presence of an acid catalyst, such as hydrogen ll-uoride. The a1- kylation effluent is then separated, usually by distillation, into linear alkylbenzenes, commonly called alkylate, and a by-product heavy alkylate. lIt is the linear alkylbenzenes which are the desired alkylate product of suicient purity to be called detergent-grade. The excess n-parans are usually recycled to the dehydrogenation section and usually any excess benzenes are recycled to the alkylation reaction zone. A more detailed description of this latter process for producing detergent-grade linear alkylbenzenes may be found in UOP Discloses New Way To Make Linear Alkylbenzenes, by Dr. Herman S. Bloch, Oil and Gas Journal, Jan. 16, 1967, pages 79-81. Those skilled in the art are directed to this literature article for additional details, the contents of which a're incorporated herein by reference.

In the practice of the latter process for producing linear alkylbenzenes, it 'was found that the various alkylate homologs could not be satisfactorily separated by distillation from the n-parafn recycle due to the fact that certain of the alkylbenzenes had the same or similar boiling point with the certain n-parain hydrocarbons. Accordingly, it was found virtually impossible to produce high purity detergent-grade alkylate particularly when the desired alkylate was a 5-homolog spread alkylate, such as C10-C14 or C11-C15. Therefore, the present invention is an improved method for performing the dehydrogenationalkylation reaction of, for example, the most recent prior art method described by Bloch, supra, for producing detergent-grade linear al'kylbenzene which may then be converted into biodegradable alkylbenzene sulfonates.

Summary of the invention Therefore, it is an object of the present invention to provide an improved method for producing detergentgrade alkyl-ate.

IIt -is :another object of this invention to provide an improved method for producing `an ralkylaromatic monoalkylate sui-table `for conversion to a detergent product.

According to the present invention, there is provided a Amethod `for producing detergent-grade alkylate which comprises the steps of: (a) continuously introducing a ii-rst fraction comprising relatively intermediate boiling range n-paraflin hydrocarbons into a dehydrogenation reaction zone maintained under conditions sufficient to convert n-paran lhydrocarbons into cor-responding straight-chain mono-olefin hydrocarbons; (b) continuously passing the hydrocarbon effluent from said dehydrogenation reaction zone yinto a benzene reaction zone maintained under conditions sucient to produce an alkylate comprising alkylbenzene hydrocarbons having .an alkyl ch-ain length corresponding to the chain length o-f said mono-olefin hydrocarbons; (c) recovering a lirst 4alkylate product cornprising alkylbenzene having an alkyl chain length corresponding -to the mono-olefin hydrocarbons produced [from said irst fraction; (d) periodically introducing a second fraction comprising relatively low boiling n-parain hydrocarbons into said dehydrogenation reaction zone in -admixture with said first Ifraction and in the yabsence of hereinafter specified thi-rd fraction; '(e) periodically :recovering a second yalkylate product comprising alkylbenzenes having an alkyl chain length corresponding to the mono-olefin hydrocarbons produced from said admixture of Step (d); (f) stopping the introduction of said second fraction as in Step y(d); 4(g) periodically in- Jtroducing a third fraction comprising relatively high boiling n-paraflin hydrocarbons into said dehydrogenation reaction zone in admixture with said first fraction and in the absence of said second fraction; |(h) periodically recovering a third alkylate product comprising alkylbenzenes having an alkyl chain length corresponding to the mono-olefin hydrocarbons produced from said admixture of Step (g); (i) stopping the introduction of said -third yfraction as in Step (g) and thereafter repeating Step (d); and, (j) blending lsaid recovered alkylate products in a manner to produce the desired detergent-grade alkylate.

Another embodiment of this invention includes the method hereinabove wherein said desired detergent-grade alkylate comprises a blend olf said second and third alkylate products.

4It is noted from the 'above description that the present invention relates to -an improved method of operation wherein the n-parain hydrocarbon feedstocks lare selective-ly segregated for charge to the olefin production unit in a manner which provides continuous operation without cross-contamination of products. In the past, the basic process, as described in the previously mentioned article, required a completely blocked-out operation in order to produce various grades of alkylates having a 3 or 4 or 5 carbon homolog spread. The avoidance of cross-contamination in such prior -art processing resulted in considerable loss production during purging of the unit in order to remove the prevously produced products and/or previously used feedstocks. However, i-t is to be noted that in the practice of this invention the relatively intermediate boiling range n-paraflin hydrocarbons, such as a C11-C13 hydrocarbon fraction, is continuously processed through the system acting as its own purge with the lighter fraction or heavier fraction being cut into the feedstock mixture depending upon the quality of the desired alky-late product. Thus, it is seen that the present invention provides flexibility in producing a variety of detergent-grade alkylates without the usual `attendant loss production time and/or product contamination problems.

'The separation of straight-chain hydrocarbons from hydrocarbon mixtures may be accomplished by any means known to those skilled in the art. However, in the practice of this invention, it is distinctly preferable to use zeolytic molecular sieves to produce high purity n-parafiin hydrocarbons from a hydrocarbon mixture, such as kerosene. One prior art process for the separation of n-paraifins using molecular sieves is shown in U.S. Patent No. 2,920,037, issued on June 5, 1960. Another example is shown in U.S. Patent N0. 2,957,927 which issued Oct. 25, 1960. Some of these prior -art processes utilize a single bed system wherein one bed is maintained on an adsorption cycle and one bed on a desorption cycle. Other processes use the concept of simulated counter-current flow by moving the points of inlet and outlet of feed streams into and out of the bed using -sorbents, such as molecular sieves. For example, such a prior art process is shown in U.S. Patent No. 2,958,589 which issued May 23, 1961. However, it is only important in the practice f this invention that the n-parain hydrocarbons be segregated into a relatively low boiling fraction, such as a C n-parain hydrocarbon of high purity; -a relatively intermediate boiling fraction, such as a C11, C12, and C13 n-paraflin hydrocarbon fraction of high purity; and a relatively high boiling fraction, such as a C14 n-parafin hydrocarbon of high purity. The preferable way of producing these required fractions for the practice of the present invention is by distillation means since the boiling point-s between these varous fractions are sufficiently different for convention-al distillation techniques to be used. However, other separation techniques known to those skilled in the Iart may be used to segregate the proper selected fractions of n-paraffin hydrocarbons lfor use as feedstock in the practice of the present invention.

The dehydrogenation lreaction lfor the production of mono-olefin hydrocarbons from the proper n-parain hydrocarbon feedstock is generally carried out in the presence of a catalytic agent. The function of the catalyst is to permit the dehydrogenation o'f the paratlins to the monoolens without isomerization of the normal paratins or the resulting mono-oletins to the corresponding branchedchain analog. 4Suitable catalytic agents Ifor use in the parain dehydrogenation reaction include the neutral oxides of the elements of Group VI `and metal sulfides and/or oxides of the metals of Group VIH of the tPeriodic 1`able. The preferable dehydrogenation catalyst comprises the noble metals or metal compounds, such as platinum and/ or palladium disposed on a mutual or basic support, such as alumina. Those skilled inthe art may find a detailed description of cataylsts for producing the preferred dehydrogenation reaction in'copending application Ser. No. 590,490 tiled Oct. 31, 1966, and the teachings of this latter copending application are -incorporated herein to the extent necessary to provide information for those skilled in the art to practice the present invention.

Typical operating conditions for the dehydrogenation reaction zone utilizing the preferred catalyst hereinabove include relatively mild conditions of temperature and pressure, such as a temperature of about 870 F. and a pressure of about 30 p.s.i.g. Suflcient hydrogen is added to the reaction zone so that a mole ratio of hydrogen to combined feed of about 8 is maintained in the dehydrogenation reaction zone. Preferably, approximately 2000 parts per million of water is present in the combined feed to the dehydrogenation reaction zone.

The total hydrocarbon etiiuent from the dehydrogenation reaction zone is preferably admixed with benzene and passed into an alkylation reaction zone utilizing a catalytic agent, such as hydrouoric acid. Typically, the olefin feedstock to the alkylation reaction contains from 10 to 15 carbon atoms per molecule, preferably, from 10 to 14 carbon atoms per molecule. This linear mono-olefin is utilized as an alkylating agent for an alkylatable compound, preferably an aromatic reactant comprising the hydrophobic group in the structure of the detergents to which this invention is ultimately directed. Suitable aromatic reactants may be selected from the group consisting of benzene, toluene, xylene, ethylbenzene, methylethylbenzene, diethylbenzene, phenol, mononitrobenzene, etc. Preferably, the aromatic reactant is benzene.

The alkylation reaction is effected in the presence of a suitable catalyst capable of promoting the condensation reaction. Generally, the catalyst incorporates an inorganic material characterized as an acid-acting compound which catalyzes the alkyl transfer reaction believed to be involved. Suitable catalysts include certain mineral acids, such as sulfuric acid containing not more than about 15% by weight of Iwater and, preferably, less than about 8% by weight of Water including used sulfuric acid catalyst recovered from the alkylation of isoparatin hydrocarbons with mono-olefin hydrocarbons; hydrofluoric acid of at least 83% by weight and containing, preferably, less than about 10% by weight of water; liquefied anhydrous hydrogen fluoride; anhydrous alkyl chloride or alkyl bromide; borontrifluorde (preferably utilized in admixture with hydrouoric acid); and other acid-acting catalysts. The catalyst particularly preferred for the present alkylation reaction is hydrogen uoride containing at least 83% by weight and, more preferably, at least by weight hydrogen fluoride.

The hydrocarbon etiiuent from the alkylation reaction zone is processed through recovery facilities which are well known to those skilled in the art and, preferably, include distillation means for separating unreacted Ibenzene which is recycled to the alkylation zone, separation of unreacted n-paraffn hydrocarbons which may be recycled to the dehydrogenation reaction zone, and the separation of the desired detergent-grade alkylate from the Description of the drawing Referring now to the drawing, a petroleum kerosene which has been substantially desulfurized by hydrogenation is charged into the system via line and subjected to extraction in zone 11, preferably, utilizing molecular sieves for the separation of normal parain hydrocarbons from the non-normal parain hydrocarbons. A typical analysis of a kerosene feed is as lfollows:

Line 10 Component: lb. moles/ hr.

iCg

n-C9 0.1 i-Cm 3 3 .6 Il-Clo i-Cu 88.2 Il-Cll i-C12 92.9

DC12 8 i-C13 76.5 n-Cla 22.5 i-C14t 49.7 n-C1. 13 .6 i-C15 18 .3 IIC15 Aromatics 72.2

Total 535.2

Lbs/hr. 91,000 M.W. 170.0 BPSD 7,790 API 45 .0 Lbs./ gal. 6.675

A rainate stream comprising non-normal paraflin hydrocarbons is withdrawn -from extraction unit 11, by conventional means not shown, and an extract phase comprising normal paraffin hydrocarbons having a carbon number from C10 to C16 is withdrawn from extraction unit 11 via line 12.. A typical analysis of the material in line 12 is as follows:

6 Lbs/hr. 17,300 M.W. 171.8 BPSD 1,570 API 55.6 Lbs/gal. 6.296

The material in line 12 is passed into rst fractionator 13 which is maintained under sufiicient conditions of temperature and pressure to produce overhead in line 14 a distillate product comprising C10 n-paran hydrocarbons. A bottoms product containing C11-C16 parain hydrocarbons is withdrawn from fractionator 13 via line 15. Typically, fractionator 13 is operated at a temperature of 215 F. in the overhead and 495 F. in the bottoms utilizing a top column pressure of about 15 p.s.i.g. Utilizing these typical operating conditions, the analysis of the material in line 14 is as follows:

Line 14 Component: lb. moles/hr. i-Cg n-Cg 0.1 i-Cm Il-Cw 9.9 i-Cu 0.1 n'Cu 1.3 i-C12 lClz u 11C13 i-CM 1'1C14 n g 1'1C15 Aromatics 0.1

Total 11.5 Lbs/hr. 1,660 M.W. 144.3 BPSD API 61.0 Lbs/gal. 6.119

A typical analysis of the material in line 15 is as follows:

Line 15 Component: lb moles/ hr.

i-Cg

1'1'C9 i-C10 1'1`C10 i-Cll Il-Cu i-C12 0.1 Il-C12 i-C13 0.1 n"C13 i-CM 0.1 n-CM 11.6

n-C15 3.7 Aromatics 0.4

Total 89.4

Lbs/hr. 15,640 M.W. 175.3 BPSD 1,415 API 55.0 Lbs/gal. 6.316

The material in line 15 is introduced into fractionator 16 which is maintained under suflicient conditions of temperature and pressure to produce a concentrate of normal paraffin hydrocarbons having from C11 through C13 carbon atoms per molecule in line 17 and producing a bottoms product comprising C14 n-parailin hydrocarbons which is withdrawn from fractionator 16 via line 18. Typical operating conditions for fractionator 16 include an overhead temperature of 380o F., a kbottoms temperature of about 465 F. with approximately atmospheric pressure being maintained therein. Operating under these typical conditions, an analysis of the material in line 17 is as follows:

Line 17 Component: lb. moles/ hr. i-C9 n-C9 Cm HClg i-Cn 11C11 i-C12 0.1 n-Clg i-C13 0.1 I1C13 l-CM Il-CM i-C Il-C15 Aromatics 0.3

Total 72.6

Lbs/hr. 12,310 M.W. 170.0 BPSD 1,120 API 56.1 Lbs/gal. 6.280

Similarly, an analysis of the material in line 18 is as follows:

L-ine 18 l'l-Clg i-C14 0.1 n-CM 1 n u l'l-C15 3.7 Aromatics 0.1

Total 16.6

Lbs/hr 3,330 M.W. 200.6 BPSD 295 API 51.5 Lbs/gal. 6.437

The material in line 18 is next introduced into fractionator 19 maintained under conditions sufficient to produce a C14 n-parain hydrocarbon concentrate which is withdrawn via line 21 and a C154- n-parafiin reject stream which is withdrawn from the system via line 20. Typical operating conditions which may be used in fractionator 19 include an overhead temperature of about 510 F. and a bottoms temperature of about 555 F. utilizing approximately atmospheric pressure in the column. Un-

der these conditions, the material in line 21 will have thc following typical analysis:

Line 21 Component: 1b. moles/hr. i-C9 n-C9 i-Clo DCm i-C11 Il-Cll lClg Il-Clg C13 I1"C13 1.1 i-C14 0.1 n-C14 10.8 i-C15 II'C15 Aromatics 0.1

Total 12.1

Lbs/hr. 2,380 M.W. 196.7 BPSD 215 API 54.7 Lbs/gal. 6.326

Similarly, the material in line 20 will have the following typical analysis:

Line 20 Component: lb. moles/ hr. i-Cg n-C9 i-Cw l-Clo i-Cu Il-Cu I1C12 i-C13 ll-Cla i-C1.1l HCM 0.8 i-C15 Il-C15 3.7 Aromatics Total 4.5

Lbs./ hr 950 M.W 211.1 BPSD API 52.5 Lbs./ gal. 6.402

Referring again to fractionator 13, the C10 n-parain hydrocarbon stream in line 14 is passed into storage tank 22 for use more fully described hereinafter. In similar fashion, the C14 n-parain hydrocarbon material in line 21 is passed into storage tank 23 for use more fully described hereinafter.

The C114C13 n-paraflin hydrocarbons concentrate stream (relatively intermediate boiling range) is passed continuously via line 17 into olen production zone 28 which is maintained under conditions substantially described hereinabove. A product stream containing corresponding linear olefin hydrocarbons comprising approximately mono-oleiins is removed from zone 28 via line 29. Of the remaining 5% of the olens, the major portion comprises dienic compounds. These olefinic materials comprise about 10% (mol basis) of the total material in line 29 with the remainder (about 90%) comprising unreacted n-parafiin hydrocarbons. A by-product of the dehydrogenation reaction is hydrogen of 96% purity which is removed from zone 28, by conventional means not shown.

The hydrocarbon effluent from dehydrogenation zone 28 in line 29 is admixed with benzene from line 30 and the mixture of mono-olefins, n-paraffins, and benzeneis passed via line 29 into alkylation unit 31 which is maintained under conditions previously described hereinabove. The hydrocarbon phase from alkylation unit 31 is passed via line 32 into fractionator 33 which is maintained under conditions suicient to separate unreacted benzenes from alkylated benzenes. The unreacted benzene is removed as a distillate product from fractionator 33 and, preferably, recycled to the alkylation unit 31 via lines 34 and 30. Typical operating conditions for the fractionator 33 includes an overhead temperature of about 200 F. and a bottoms temperature of about 455 F. while maintaining a pressure of about p.s.i.g. in the bottom of the column. Operating under these conditions, the material in line 34 will have the following analysis:

Line 34 Component: lb. moL/hr. Benzene 175.58 Non-aromatics 9.61

Total 185.1;9

Lb./hr. 14,522

BPD 1,133

Lbs/gal 7.33

Similarly, the material in line 35 which comprises alkylbenzenes and parans will have the following typical analysis:

The material in line 35 comprising n-para'in hydrocarbons admixed with alkylbenzenes is introduced from line 35 into fractionator 36 which is maintained under conditions sufcient to separate the normal paraffin hydrocarbons from the alkylbenzenes. The normal parains are withdrawn from fractionator 36 via line 37 and, preferably, recycled to olefin production unit 28 in admixture with the material in line 17. Typical operating conditions for fractionator 36 include an overhead temperature of about 285 F. and a bottoms temperature of about 485 F. while maintaining a pressure of about 200 mm. Hg absolute in the bottom of the column. Operating under these conditions, the material in line 37 will have the following analysis:

Line 37 Component: lb. moL/hr. n-P 11 n-P12 l'lPla Iso-l-cyclics 24 Aromatics 12 Total 683 Similarly, the material in line 38 will have the following analysis:

Line 38 Component: lb. mol./hr. n-Pu alkylbenzene 24 n-P12 alkylbenzene 27 n-P13 alkylbenzene 2l Other D.A 2 Heavy alkylate 3 Total 77 The alkylbenzene material in line 38 is introduced into rerun column or fractionator 39 for the separation of the desired alkylate product which is removed via line 41 and passed subsequently into proper segregated storage. A reject stream comprising heavy alkylate is withdrawn from fractionator 39 via line 40. Typical operating conditions for fractionator 39 include an overhead temperature of about 360 F. and a bottoms temperature of about 550n F. while maintaining a pressure of about 15 mm. Hg absolute in the top of the column. For the tlow scheme just described, the material in line 41 comprises an alkylbenzene having from C11-C13 carbon numbers in the alkyl side-chain, .e., a 3-carbon number homolog spread in the alkyl side-chain.

While processing the material continuously in line 17, control valves 25 and 27 are in a closed position.

Periodically control valve 25 is open, thereby introducing relatively light normal parain hydrocarbons from storage tank 22 via line 24 into line 17 for `admixture with the relatively intermediate boiling range normal parain hydrocarbons which are continuously being processed through the system from line 17. The admixture of material from line 24 and line 17 is processed through olefin production unit 31 under substantially the same conditions previously described hereinabove. However, in this case, the desired alkylate product being removed to segregated storage (not shown) via line 41 contains alkylbenzene having a C10-C13 carbon number alkyl side-chain, i.e. a 4-carbon number homolog spread in the alkyl side-chain. For this case, the four carbon number homolog spread in line 41 is designated broadly as a second alkylate product while the material produced from only C10-C13 parain hydrocarbons in line 17 is designated broadly as a rst alkylate product.

The introduction of the relatively light normal paraflin hydrocarbons is stopped at a predetermined time by closing valve 25. Operation of the plant continues by the continuous introduction of material from line 17 through the various processing units for a time sufficient to purge these units of the feedstock and products produced during the cycle in which material from line 24 was being processed. With valve 25 and 27 closed, the operation of purging continues with the segregation of material from line 41 being sent to storage as the iirst alkylate product.

Following purging of the unit with the material only from line 17 and with valve 25 closed for a sufficient predetermined amount of time, valve 27 is now open permitting the passage of relatively heavy n-para'lin hydrocarbons from storage tank 23 via line 26 into line 17 in admiXture with the relatively intermediate boiling range n-parafn material. Thus, the admixture of relatively intermediate material and relatively heavy material is now processed through olefin production unit 28, alkylation unit 31 into subsequent separation facilities in substantially the same manner and under substantially the same conditions as previously described for processing only the material in line 17. However. in this latest case, the alkylbenzene product being removed in line 41 now designated broadly as a third alkylate product contains alkylbenzenes having from C11-C14 in the alkyl side-chain, i.e. a four carbon number homolog spread in the alkyl side-chain. This relatively heavy alkylate material in line 41 is sent to segregated storage (not shown).

Depending upon the demands of the market place, the various segregated alkylate products are now blended to produce the desired alkylate product. For example, a blend of the second alkylate product and the third alkylate product will produce a desired alkylate product of detergent-grade quality having a S-carbon number homolog spread, i.e. C10-C14 carbon numbers in the alkyl sidechain. In other words, in the latter example, the desired detergent-grade alkylate comprises a mixture of alkylbenzene hydrocarbons containing from C10-C14 carbon atoms in the alkyl side-chains.

For convenience, the various segregated storage facilities for the various alkylate products have not been shown in the appended drawing. Those skilled in the art know well how to construct such segregated storage and blending facilities.

The invention claimed:

1. Method for producing detergent-grade alkylate which comprises the steps of (a) continuously introducing a rst fraction comprising relatively intermediate boiling range n-paran hydrocarbons into a dehydrogenation reaction zone maintained under conditions suflicient to convert n-parain hydrocarbons into corresponding straightchain mono-olefin hydrocarbons;

(b) continuously passing the hydrocarbon eiuent from said dehydrogenation reaction zone into a benzene alkylation reaction zone maintained under conditions suicient to produce an alkylate comprising alklbenzene hydrocarbons having an alkyl chain length corresponding to the chain length of said mono-oleiin hydrocarbons;

(c) recovering a first alkylate product comprising alkylbenzenes having an alkyl chain length corresponding to the mono-olefin hydrocarbons produced from said first fraction',

(d) periodically introducing a second fraction comprising relatively low boiling n-paraiiin hydrocarbons into said dehydrogenation reaction zone in admixture with said rst fraction and in the absence of hereinafter specified third fraction;

(e) periodically recovering a second alkylate product comprising alkylbenzenes having an alkyl chain length corresponding to the mono-olefin hydrocarbons produced from said admixture of Step (d);

(f) stopping the introduction of said second fraction as in Step (d);

(g) periodically introducing a third fraction comprising relatively high boiling n-paratlin hydrocarbons into said dehydrogenation reaction zone in admixture with said tirst fraction and in the absence of said second fraction;

(h) periodically recovering a third alkylate product comprising alkylbenzenes having an alkyl chain length corresponding to the mono-olefin hydrocarbons produced from said admixture of Step (g);

(i) stopping the introduction of said third fraction as in Step (g) and thereafter repeating Step (d); and,

(j) blending said recovered alkylate products in a manner to producethe desireddetergent-grade alkylate.

2. Method according to claim 1 wherein said desired detergent-grade alkylate comprises a blend of said second and third alkylate products.

3. Method according to claim 1 wherein said first fraction comprises C11 to C13 n-parain hydrocarbons, said second fraction comprises C10 n-parafin hydrocarbons, and said third fraction comprises C14 n-parain hydrocarbons.

4. Method according to claim 3 wherein said desired detergent-grade alkylate comprises a mixture of said a1- kylbenzene hydrocarbons containing from C10-C14 carbon atoms in the alkyl chain.

References Cited UNITED STATES PATENTS 3,320,714 5/ 1967 Rubinfeld 260--671 3,349,141 10/1967 Sweeney 260-668 3,358,047 12/1967 Liston 260-668 DELBERT E. GANTZ, Primary Examiner.

CURTIS R. DAVIS, Assistant Examiner. 

